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WO1995017265A1 - Concentre de colorant polymere a base d'halogenure de vinyle - Google Patents

Concentre de colorant polymere a base d'halogenure de vinyle Download PDF

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Publication number
WO1995017265A1
WO1995017265A1 PCT/US1994/014017 US9414017W WO9517265A1 WO 1995017265 A1 WO1995017265 A1 WO 1995017265A1 US 9414017 W US9414017 W US 9414017W WO 9517265 A1 WO9517265 A1 WO 9517265A1
Authority
WO
WIPO (PCT)
Prior art keywords
set forth
vinyl halide
compatibilizer
halide polymer
microns
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US1994/014017
Other languages
English (en)
Inventor
Surachai Wimolkiatisak
Dennis L Hammond
Anthony S. Scheibelhoffer
Allen W. Carlson
Mir L. Ali
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Vibrantz Corp
Original Assignee
Ferro Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Ferro Corp filed Critical Ferro Corp
Priority to EP95903686A priority Critical patent/EP0684876A4/fr
Priority to AU12661/95A priority patent/AU1266195A/en
Publication of WO1995017265A1 publication Critical patent/WO1995017265A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J3/00—Processes of treating or compounding macromolecular substances
    • C08J3/20—Compounding polymers with additives, e.g. colouring
    • C08J3/22—Compounding polymers with additives, e.g. colouring using masterbatch techniques
    • C08J3/226—Compounding polymers with additives, e.g. colouring using masterbatch techniques using a polymer as a carrier
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J3/00—Processes of treating or compounding macromolecular substances
    • C08J3/20—Compounding polymers with additives, e.g. colouring
    • C08J3/203—Solid polymers with solid and/or liquid additives
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2327/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers
    • C08J2327/02—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers not modified by chemical after-treatment
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2427/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers

Definitions

  • the present invention concerns a color concentrate for use in coloring plastics. More particularly, the present invention concerns a dustless solid color concentrate comprising a vinyl halide polymer resin core and a colorant material additive shell.
  • the traditional method for incorporating dry colors and additives into a thermoplastic polymer to produce a color concentrate involves blending the polymer with the color and additives in a melt, the melt being formed in an extruder or a batch type mixer such as a Banbury mixer.
  • the disadvantages associated with these techniques include appreciable downtime for cleaning the equipment, high-energy costs for running the equipment, and long production cycles. Additionally, with respect to some polymer resins, the traditional method of processing can lead to the degradation of the polymer and/or the creation of an undesirable heat history.
  • Aubrey et al. discloses a method for preparing coated resin granules wherein a mixture of resin granules, a wax and a particulate material is subjected to high-intensity blending at elevated temperatures.
  • the Aubrey et al. process is applicable to a variety of thermoplastic resins including polyolefins, vinylidene polymers, polyamides and other polymers.
  • One disadvantage associated with the Aubrey et al. process is that the wax employed has to be melted for the process to work.
  • the wax may be considered in some applications to be a costly additive and/or an undesirable additive.
  • waxes can melt in the screw of an extruder or injection molding machine and this can cause lubrication of the screw and loss of production efficiency or rate.
  • Another method for incorporating color and additives into a polymer resin is described in Chatterjee et al. , European Patent Publication No. 0,471,463A2. Chatterjee et al. discloses the use of high-speed impingement to incorporate color and additives into a polymer resin. This process, like the process disclosed in Aubrey et al. , may be used to process a variety of polymers.
  • a disadvantage associated with this process is that it requires the melting of the additive and/or the surface of the polymer resin to promote the incorporation of the additive into the polymer resin. If the processing temperature is higher than the optimum temperature, the entire polymer resin particle can melt, resulting in a large molten mass or a large proportion of agglomerates instead of a uniform powder size.
  • Pennie et al. Another method for incorporating color and additives into a polymer resin is described in Pennie et al. , U.S. Patent No. 4,375,520.
  • the method comprises the mixing in a Papenmeir mixer of a liquid polymeric substance and a low molecular weight polymer having a melting point in the range of about 95°C to 105°C.
  • Pennie et al. is specific to the use of a polymer having a melting point of about 95°C to 105°C and the process is conducted at or near the melting point of the polymer.
  • Pennie et al. does not provide any insight into how to process a primarily amorphous polymer resin that does not display a melting point, such as poly(vinyl chloride) (PVC) .
  • PVC poly(vinyl chloride)
  • the present invention provides a new and improved method of producing a dustless vinyl halide polymer color concentrate that does not require the formation of a hot melt or the use of wax.
  • the color concentrate comprises a multitude of fine particles which each comprise a vinyl halide polymer resin core and a colorant material shell.
  • the method includes the steps of providing a vinyl halide polymer, providing a colorant material, providing a compatibilizer having a solubility parameter of from about 7 to about 12 (cal/ml) 1/2 , and mixing the vinyl halide polymer, compatibilizer and colorant material together to yield the dustless concentrate in the form of a vinyl halide resin core surrounded by a shell of the compatibilzer and the colorant material.
  • the vinyl halide polymer comprises poly(vinyl chloride) (PVC) and the compatibilizer comprises epoxidized soybean oil.
  • Color concentrates made in accordance with the principles of the present invention yield various advantages. These advantages include for example: (i) the production of a non- dusting, free flowing, uniform particle size concentrate; (ii) the production of a concentrate that provides good dispersion when added to the thermoplastic being colored; (iii) the absence of melt extrusion or melt formation during production of the concentrate which can create an undesirable heat history; (iv) the absence of costly waxes that may cause processing problems or detrimental properties; (v) batch size flexibility; (vi) no screw slippage when the concentrate is added to an extruder; (vii) faster color changes; (viii) the absence of additives or other materials that can be detrimental to the properties of the vinyl halide polymer resin; and (ix) good yields during the production of the concentrate.
  • the method comprises the steps of providing a vinyl halide polymer resin, providing a compatibilizer having a solubility parameter of from about 7 to about 12 (cal/ml) 12 , providing one or more colorant materials, and mixing the polymer resin, colorant and compatibilizer in a mixing device such as a Henschel mixer.
  • the vinyl halide polymer resin may comprise one or more of the commercially available polymer resins.
  • Such polymers include, for example, poly(vinyl chloride) including homopolymers and copolymers thereof, alloys and blends comprising homopolymers and copolymers of poly(vinyl chloride), poly(vinyl fluoride) including homopolymers and copolymers thereof, poly(vinylidene dichloride) including homopolymers and copolymers thereof and chlorinated poly(vinyl chloride) including homopolymers and copolymers thereof.
  • the vinyl halide polymer resin preferably has an average particle size in the range of about 70 microns to about 500 microns. More preferably, the vinyl halide polymer resin has a particle size in the range of about 150 microns to about 250 microns.
  • the compatibilizer is a material that is liquid below
  • the compatibilizer has a solubility parameter of from about 7 to about 12 (cal/ml) 1/2 . More preferably, the compatibilizer has a solubility parameter of from about 8.5 to about 10.5 (cal/ml) 12 .
  • compatibilizers examples include epoxidized soybean oil, epoxidized tall oil, epoxidized linseed oil, ethoxylated sorbitan trioleate, sorbitan trioleate, tri-iso-octyl phosphate, octyl diphenyl phosphate, tolyl diphenyl phosphate, tritolyl phosphate, trixylyl phosphate, triphenyl phosphate, di-n-butyl phthalate, di-2-ethylhexyl phthalate, di-n-hexyl phthalate, di-iso-octyl phthalate, di-n-octyl phthalate, di- isodecyl phthalate, di-tridecyl phthalate, n-Butyl benzyl phthalate, di-2-methoxyethyl phthalate, butyl butoxycar- bonylmethyl phthalate, di-2-
  • the colorant material may comprise any one or more of a number of commercially available colors or pigments.
  • colorant material means any conventional inorganic or organic pigment or organic dyestuff. Such materials are described, for example, in Kirk- Othmer Encyclopedia of Chemical Technology, Third Edition, Vol. 6, pp. 597-617, which is incorporated herein by reference.
  • inorganic pigments include, for example, titanium dioxide, iron oxide, zinc chromate, cadmium sulfides, chromium oxides and sodium aluminum silicate complexes.
  • organic type pigments include azo and diazo pigments, phthalocyanines, quinacridone pigments, perylene pigments, isoindolinone, anthraquinones, thioindigo and solvent dyes.
  • additives may include, for example, stabilizers such as alkaline earth metal soaps and carboxylates such as calcium benzoate, calcium octoate and calcium naphthenate, Friedel-Crafts cation progenitor compounds such as zinc oxide, zinc hydroxide, zinc carbonate, zinc acetate, zinc laurate, zinc naphthenate, zinc stearate, zinc oleate, zinc 2-ethyl- hexoate, cadmium oxide, cadmium hydroxide, cadmium carbonate, cadmium acetate, cadmium laurate, cadmium naphtheneate, cadmium stearate, cadmium oleate, cadmium 2-ethyl-hexoate, calcium stearate, aluminum oxide, aluminum hydroxide, aluminum carbonate, aluminum acetate, aluminum chlorolaurate, antimony oxide, antimony hydroxide, antimony
  • fillers and/or reinforcers may also be included in the process.
  • Such fillers and/or reinforcers include, for example, CaC0 3 , talc, glass, clay and mica.
  • the portions of vinyl halide polymer resin, color and compatibilizer can vary quite a bit.
  • the mixture utilized comprises from about 20 to about 60 weight percent vinyl halide polymer, from about 5 to about 20 weight percent compatibilizer and from about 25 to about 75 weight percent colorant material.
  • the mixture may comprise up to 15 weight percent additive.
  • the mixture comprises from about 25 to about 55 weight percent vinyl halide polymer, from about 10 to about 15 weight percent compatibilizer, and from about 30 to about 70 weight percent colorant material.
  • Various high-intensity mixing devices may be utilized in accordance with the principles of the present invention. Such devices include, for example, Papenmeir mixers, Waring blenders and Henschel mixers. Preferably, a Henschel mixer is employed.
  • the mixing device is operated at a tip speed of from about 10 to about 60 meters/second.
  • the mixing device is operated at a tip speed of from about 20 to about 40 meters/second.
  • an additive it is best when producing the concentrate to first mix the additive with the vinyl halide polymer resin for a brief period such as 10 to 20 seconds.
  • the colorant material then can be added and mixed for 10 to 20 seconds.
  • the compatibilizer is then added and mixed for 3 to 10 minutes.
  • these are merely general mixing times and the actual mixing times will depend on such variables as, for example, the size of the mixing container, the amount and type of materials being mixed and the speed and configuration of the mixing blade.
  • the mixing should be conducted until a temperature of from about 140°F to about 180°F is reached, and preferably from about 150°F to about 180°F is reached.
  • metal stearates such as calcium stearate
  • Addition of metal stearates to the mixer may result in the formation of a fragile ball. However, such ball will readily break up into free-flowing particles with a gentle tap.
  • After mixing the mixture is generally passed through a sieve in order to remove oversize aggregates. Generally, a yield of over 90% by weight is attained. After sieving the mixture comprises a non-dusting, free-flowing, uniform particle size concentrate.
  • the concentrate generally comprises a multitude of particles having an average particle size of from about 150 to about 850 microns.
  • Each particle comprises a vinyl halide polymer resin core and an outer coating of compatibilizer, colorant materials and additives.
  • the resin cores have a diameter of from about 70 microns to about 500 microns.
  • let-down resins can be used in connection with the color concentrates of the present invention.
  • the let-down resin can be either flexible or rigid PVC compounds or any other polymers compatible with the vinyl halide resin used to produce the color concentrate.
  • the color concentrates of the present invention are used in the same manner as conventional concentrates (i.e., dry blending with the let-down resin followed by extrusion) .
  • Let-down ratios vary depending on the desired colors and applications. In general, the ratio ranges from about 10:1 to about 100:1.
  • the ultimate color of the color concentrate can be easily controlled or corrected. More particularly, before adding the compatibilizer one can conduct a color check on the colorant material and vinyl halide polymer resin using any one of a number of conventional techniques, such as, for example, melt mixing with the let ⁇ down resin. If the color of the melt is found to be unacceptable, additional colorant materials can be added during manufacture prior to the addition of the compatibilizer so as to adjust the color as required.
  • Example I The following components were charged into a FM150 Henschel mixer having a 150 litre mixing chamber. The mixer was operated at a tip speed of 20 meters/second using a variant-type mixing blade. Component Weight % Weight
  • Epoxidized soybean oil 9.5 9.025 lbs.
  • the PVC and the THERM-CHEK 840 stabilizer are mixed separately for 15 seconds.
  • the calcium stearate and mixed metal pigment are then added and mixed for 15 seconds.
  • the epoxidized soybean oil is then gradually added and mixed for five minutes yielding a mixture of free-flowing fine particles.
  • the fine particles are then passed through a 20 mesh screen yielding about 2% oversized particles that do not pass through the screen.
  • the sieved particles are ready for use as a color concentrate.
  • the oversize particles can be ground and used in subsequent batches without causing any detrimental effects.
  • Example II The following components were charged into a FM150
  • Henschel mixer having a 150 litre mixing chamber.
  • the mixer was operated at a tip speed of 20 meters/second using a variant-type mixing blade.
  • the PVC and the THERM-CHEK 840 stabilizer are mixed separately for 15 seconds. 1.9 pounds of the calcium stearate, the carbon black, the ethylene bis-stearamide and the calcium carbonate are then gradually added and mixed for 15 seconds. The epoxidized soybean oil is then added and mixed for about 5 minutes. Finally, .48 pounds of the calcium stearate is added and mixed for 30 seconds to eliminate smearing. The calcium stearate added in the final step coats each of the fine particles that are produced. The fine particles are then passed through a 20 mesh screen yielding about 2% oversize particles that do not pass through the screen. The sieved particles are ready for use as a color concentrate. The oversized particles can be ground and used in subsequent batches without causing any detrimental effects.
  • Example III Example III
  • Example II The color concentrate made as described in Example I was used at a 33:1 let-down ratio with a white rigid PVC compoun The two materials were dry blended and melt extruded to make a 1" diameter gray PVC pipe. The materials extruded well and the pipe has good appearance with good pigment dispersion.
  • Example IV The color concentrate made as described in Example II was used at a 20:1 let-down ratio with a white rigid PVC compound. The two materials were dry blended and melt mixed on a two- roll mill to make a gray PVC sheet. The materials processed well and the sheet had good appearance with good pigment dispersion.

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  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Processes Of Treating Macromolecular Substances (AREA)
  • Compositions Of Macromolecular Compounds (AREA)

Abstract

Nouveau procédé amélioré de production de concentrés de colorant consistant en un polymère d'halogénure de vinyle exempt de poussière, ne nécessitant pas de formation de fusion ni l'utilisation de cires. Ce concentré comporte une multitude de particules fines dont chacune se compose d'un noyau dudit polymère et d'une enveloppe de colorant. Le procédé comporte les étapes suivantes: 1) se procurer le susdit polymère, le colorant et un agent de compatibilité présentant un taux de solubilité compris entre environ 7 et environ 12 (cal/ml) 1/2; et 2) les mélanger de façon à obtenir un concentré exempt de poussière se présentant sous la forme d'un noyau de résine d'halogénure de vinyle entouré d'une enveloppe d'un agent de compatibilité et de colorant.
PCT/US1994/014017 1993-12-20 1994-12-05 Concentre de colorant polymere a base d'halogenure de vinyle Ceased WO1995017265A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP95903686A EP0684876A4 (fr) 1993-12-20 1994-12-05 Concentre de colorant polymere a base d'halogenure de vinyle.
AU12661/95A AU1266195A (en) 1993-12-20 1994-12-05 Vinyl halide polymer color concentrate

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US17046093A 1993-12-20 1993-12-20
US08/170,460 1993-12-20

Publications (1)

Publication Number Publication Date
WO1995017265A1 true WO1995017265A1 (fr) 1995-06-29

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Family Applications (1)

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PCT/US1994/014017 Ceased WO1995017265A1 (fr) 1993-12-20 1994-12-05 Concentre de colorant polymere a base d'halogenure de vinyle

Country Status (5)

Country Link
US (1) US5843524A (fr)
EP (1) EP0684876A4 (fr)
AU (1) AU1266195A (fr)
CA (1) CA2155670A1 (fr)
WO (1) WO1995017265A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7347929B2 (en) 2003-12-05 2008-03-25 Intercat, Inc. Gasoline sulfur reduction using hydrotalcite like compounds
US7361264B2 (en) 2004-06-02 2008-04-22 Intercat, Inc. Mixed metal oxide additives
US7361319B2 (en) 2003-12-05 2008-04-22 Intercat, Inc. Mixed metal oxide sorbents

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ES2137460T3 (es) * 1994-08-29 1999-12-16 Cabot Corp Mezcla basica universal.
US6646038B1 (en) * 1999-08-30 2003-11-11 Ferro Corporation Color concentrate
US6194507B1 (en) 1999-08-30 2001-02-27 Ferro Corporation Metal filled concentrate
EP1273412A1 (fr) * 2001-07-02 2003-01-08 Magma Trade di Mauro Magni & C.snc Procédé et dispositif pour la fabrication des polymères thermoplastiques chargés
US20060091578A1 (en) * 2004-11-02 2006-05-04 Bravo Juan M Wood-polymer composites and additive systems therefor
CN102348743A (zh) * 2009-03-09 2012-02-08 安德斯·弗伦伯格 制备母料和复合物的方法
WO2012102672A1 (fr) * 2011-01-26 2012-08-02 Lambdainnovation Pte. Ltd. Compositions et procédés pour la protection de béton armé
CN102977511B (zh) * 2012-12-11 2014-08-13 上海一品颜料有限公司 用于聚氯乙烯塑料加工的色砂
KR102519574B1 (ko) * 2020-09-25 2023-04-07 에스케이이노베이션 주식회사 코어-쉘 구조를 가지는 PVDC (Polyvinylidene chloride)계 복합체 및 이의 제조방법

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US3591409A (en) * 1969-07-28 1971-07-06 Monsanto Co Process for coating resin granules by high intensity mechanical blending and product obtained thereby
US3819560A (en) * 1972-01-06 1974-06-25 Minnesota Mining & Mfg Vinyl halide polymer/epoxide resin powder coating compositions
US4375520A (en) * 1981-04-10 1983-03-01 Dart Industries Inc. Densification of particulate materials
US4495128A (en) * 1979-06-14 1985-01-22 Wavin B.V. Method for coloring polyvinylchloride
CA2006350A1 (fr) * 1988-12-27 1990-06-27 Richard Francois Theodor Bes Methode pour l'obtention d'une composition pulverulente renfermant un colorant et (ou) un pigment
US5066422A (en) * 1988-06-03 1991-11-19 Armstrong World Industries, Inc. Static dissipative vinyl surface covering materials, methods for them, and composition for static dissipation
EP0471463A2 (fr) * 1990-07-31 1992-02-19 Shell Oil Company Procédé pour mélanger des additifs dans des polymères thermoplastiques
US5139817A (en) * 1990-03-14 1992-08-18 Sumitomo Chemical Co., Ltd. Method for surface treating and coating thermoplastic resin shaped articles
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US3591409A (en) * 1969-07-28 1971-07-06 Monsanto Co Process for coating resin granules by high intensity mechanical blending and product obtained thereby
US3819560A (en) * 1972-01-06 1974-06-25 Minnesota Mining & Mfg Vinyl halide polymer/epoxide resin powder coating compositions
US4495128A (en) * 1979-06-14 1985-01-22 Wavin B.V. Method for coloring polyvinylchloride
US4375520A (en) * 1981-04-10 1983-03-01 Dart Industries Inc. Densification of particulate materials
US5066422A (en) * 1988-06-03 1991-11-19 Armstrong World Industries, Inc. Static dissipative vinyl surface covering materials, methods for them, and composition for static dissipation
CA2006350A1 (fr) * 1988-12-27 1990-06-27 Richard Francois Theodor Bes Methode pour l'obtention d'une composition pulverulente renfermant un colorant et (ou) un pigment
US5139817A (en) * 1990-03-14 1992-08-18 Sumitomo Chemical Co., Ltd. Method for surface treating and coating thermoplastic resin shaped articles
EP0471463A2 (fr) * 1990-07-31 1992-02-19 Shell Oil Company Procédé pour mélanger des additifs dans des polymères thermoplastiques
US5264280A (en) * 1992-09-21 1993-11-23 Ferro Corporation Multilayer thermoformable structure

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7347929B2 (en) 2003-12-05 2008-03-25 Intercat, Inc. Gasoline sulfur reduction using hydrotalcite like compounds
US7361319B2 (en) 2003-12-05 2008-04-22 Intercat, Inc. Mixed metal oxide sorbents
US7361264B2 (en) 2004-06-02 2008-04-22 Intercat, Inc. Mixed metal oxide additives

Also Published As

Publication number Publication date
EP0684876A4 (fr) 1996-06-05
AU1266195A (en) 1995-07-10
US5843524A (en) 1998-12-01
CA2155670A1 (fr) 1995-06-29
EP0684876A1 (fr) 1995-12-06

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